BRPI0711043A2 - processes and apparatus for preparing an aminoalkylnitrile, and for preparing a diamine, and use of an apparatus - Google Patents

Abstract

PROCESSES AND APPARATUS FOR PREPARING AN AMINOalkylNITRILLA, AND FOR PREPARING A DIAMINE, AND, USE OF AN APPLIANCE The present invention relates to processes for preparing an aminoalkyl nitrile by reacting a corresponding monoamine with a corresponding alkenyl nitrile in a continuous manner, comprising the steps of: (a) feeding the monoamine corresponding to a continuous reaction current; (b) feeding the alkenyl nitrile corresponding to a reaction stream, which already contains the added aminoalkyl nitrile; (c) converting the reaction stream into a first reaction region; and (d) at least partially transferring the reaction stream to at least a second reaction region for another conversion. The invention also relates to processes for preparing an aminoalkylnitrile diamine, the apparatus suitable for carrying out the processes, and their corresponding use.

Description

"PROCESSES AND APPARATUS FOR PREPARING AN ALKINE, AND FOR PREPARING A DIAMINE, AND USING AN APPLIANCE"

The present invention relates to processes for preparing an aminoalkylnitrile by reacting a corresponding monoamine with a corresponding alkenylnitrile, and also to a process for preparing a diamine of such an aminoalkylnitrile, and also the apparatus that can be used to perform the processes.

Diamines are an important group of chemicals, which are used in a wide variety of media such as starting materials, intermediates or end products.

3-Dimethylaminopropylamine (DMAPA, N, N-dimethyl-1,3-diaminopropane), in particular, is an important intermediate for industrial production of, for example, liquid soaps. In addition, DMAPAserve is a starting material for the preparation of coagulants and is further referred to as having anti-corrosion properties.

Diamines, like their amine analogs, are often prepared by reducing nitriles. This reaction is particularly advantageous when primary amines are to be obtained.

Corresponding nitriles, which may already have an amino function, are obtained, for example, from alkenylnitriles by the addition of a monoamine in a C-C double bond.

It is particularly advantageous that an integrated production process or integrated apparatus may be used for the preparation of nitrile diamines. Here, the product stream first obtained, which comprises aminonitrile, is used either directly or after purification for diamine conversion in another step.

Here, the quality of the first reaction aminoalkylnitrile product stream (monoamine and alkenylnitrile) is of critical importance for the nitrile reduction reaction, especially for the consumption of the catalyst used in the reduction.

In the case of 3-dimethylaminopropylamine, the preparation of 3-dimethylaminopropionitrile (DMAPN) is therefore important with the latter being prepared from acrylonitrile and dimethylamine. The literature describes integrated processes, in particular for preparing DMAPA, which comprise both the addition and reduction steps. In addition, optimized processes are described for each of the individual steps.

These processes can be primarily divided into processes that are carried out in batch or at least semi-finished, and processes that can be performed in a continuous mode of operation.

An integrated production process whereby, for example, DMAPA can be prepared in batches, is described in German patent application number 10 2005 052 457.5, which was filed by the applicant.

However, it has been found to be advantageous to provide continuous processes as an alternative to such at least partially batch processes. Here, it is particularly important to provide a process for the first stage that is optimized for the second stage (reduction) so that the production of the optimized diamine is similarly achieved in the second stage (reduction).

In this context, a high degree of optimization in particular means that a high individual or total diamine production is obtained. In addition, it is important for the production to be obtained with a very high individual or total conversion. Moreover, another quality criterion is that of spacetime productions with which such a process can be performed. Finally, the consumption of the catalyst used in the reduction also plays an important role.

A process for preparing 3-dimethylaminopropionitrile is described, for example, in DD-A 58 306. In this, it is proposed that previously formed 3-dimethylaminopropionitrile be used as an edible solvent in the reaction of acrylonitrile with dimethylamine to obtain, because of of the exothermic reaction and the boiling behavior of dimethylamine, a necessary improved heat distribution and removal. This is referred to as increasing the production of 3-dimethylaminopropionitrile.

DD-A 222 011 describes a process for the continuous preparation of DMAPN, in which the reaction components are, in the liquid state, first placed in a mixing chamber in a tube reactor and then mixed in stages and reacted in stages through the length. reactor total.

Finally, DE-A 27 09 966 describes the preparation of DMAPN, but in this dimethylamine is used in gaseous form and the reaction is carried out in a bubble column reactor in which the reagents are countercurrently conducted.

Although optimized processes are known in the prior art, there is still a need to provide other processes and corresponding apparatus to optimize the preparation of an aminoalkylnitrile and / or the resulting preparation of a diamine.

It is therefore an object of the present invention to provide processes and apparatus for such optimization.

The object is achieved by a process for preparing an aminoalkylnitrile by reacting a corresponding monoamine with a corresponding alkenylnitrile in a continuous mode of operation comprising the steps

(a) feeding of monoamine corresponding to a continuously conducted reaction current;

(b) feeding the corresponding alkenylnitrile into a reaction chain which already comprises the aminoalkylnitrile in addition, (c) reacting the reaction current in a first deriving region, and

(d) at least partially transferring the reaction current to at least one second reaction region for another reaction.

It has been found to be advantageous, especially in the continuous mode of operation, not to add alkenylnitrile to pure monoamine and furthermore to separate the reaction regions so that the reaction can be performed in at least two stages.

The optimized process described above has the additional advantage that it is possible to obtain an aminoalkylnitrile stream which is particularly suitable for use in the subsequent reduction of the corresponding nitrile nadiamine.

The process of the invention for preparing an aminoalkyl nitrile is thus based on the addition reaction in which a primary or secondary monoamine is added at the C-C double bond of an alkenyl nitrile.

For the purposes of the present invention, the terms "corresponding alkenylnitrile" and "corresponding monoamine" means that these are selected such that aminoalkylnitrile having the desired structural formula is obtained after the synthesis step described above.

For example, if alkenylnitrile is acrylonitrile (ACN) and ammonamine is dimethylamine (DMA), the reaction of the starting materials gives the desired 3-dimethylaminopropionitrile (DMAPN). In other words, if DMAPN is to be obtained in the process of the invention, it can be clearly observed that the corresponding alkenylnitrile is ACN and the corresponding monoamino is DMA.

Alkenyl nitrile is preferably a C 2 -C 4 alkylene which may be straight or branched and wherein a hydrogen atom has been substituted by the cyano group.

The term C 2 -C 4 alkylene refers to an alkylene having from 2 to 4 carbon atoms and comprising at least one CC double bond. Preference is given that precisely one CC double bond is present at the α, β position relative to the cyano group. . Examples of C 2 -C 4 alkenes are ethylene, propene, 1-butene, 2-butene, 2-methylpropene.

Examples of alkenylnitriles are acrylonitrile, but-2-enenitrile, methacrylonitrile, pent-2-enenitrile, 2-ethylacrylonitrile, 2-methylbut-2-enenitrile and 3-methylbut-2-enenitrile.

Preference is given to ACN.

Monoamine is preferably a secondary or secondary amine of the general formula R 1 R 2 NH, wherein R 1, R 2 are each independently H or C 1 -C 4 alkyl, provided that at least one radical R 1, R 2 is not hydrogen. .

C 1 -C 4 alkyl is methyl, ethyl, n-propyl, i-propyl, 1-n-butyl, 2-n-butyl, i-butyl, t-butyl.

Preference is given to DMA. In a particular embodiment, aminoalkylnitrile is 3-dimethylaminopropionitrile.

The process of the invention for preparing aminoalkyl nitrile must be carried out in a continuous mode of operation. This makes the conversion particularly efficient along with the high possible spacetime production.

Accordingly, in steps (a) and (b) of the invention process, for preparing an aminoalkylnitrile, introduction of the corresponding monoaminacryl and introduction of the corresponding alkenylnitrile are performed in a continuously conducted reaction stream. Here, care has been taken to ensure that the corresponding alkenylnitrile is introduced into the reaction chain in a manner such that it already comprises aminoalkylnitrile in addition. This ensures that the monoamine present in the reaction current is, if appropriate, present in sufficient dilution as the reaction heat evolved upon the addition of alkenylnitrile and can be properly controlled. This can also be achieved by the current stripping after introduction of the corresponding alkenylnitrile which is passed through a heat exchanger so as to be able, if appropriate, to remove heat. The actual reaction of monoamine with alkenylnitrile occurs in a first reaction region. This first reaction region may be a zone in a reactor, or a reactor as such.

The reaction region is typically distinct from the line regions which are merely for introducing or discharging the reaction current by the time the current stays in the respective regions. The average residence time in a reaction region is preferably more than 15 minutes, more preferably more than 30 minutes, with the average residence time for line regions generally being less than 10 minutes.

In addition, at least partial transfer of the strand current into at least one second reaction region which is physically separated from the first reaction region occurs for the purposes of another reaction in the process of the invention to prepare an aminoalkylnitrile. The second reaction region may be another zone in the aforementioned reactor or another reactor or cascade of reactors. Physical separation of the first and second reaction regions may be effected, for example, by means of tubes.

It is advantageous for the entire reaction stream not to be transferred to at least one second reaction region, but rather part of the reaction chain comprising already formed aminoalkylnitrile to be recycled so that the corresponding monoaminacent and corresponding alkenylnitrile can each will be introduced into the reaction stream comprising aminoalkylnitrile after at least the beginning of aminoalkylnitrile formation in the first deriving region.

A preferred embodiment of the process of the invention for preparing an aminoalkylnitrile therefore comprises performing at least steps (a) to (c) of the process of the invention for preparing an aminoalkylnitrile in the recycle mode.

Furthermore, it has been found to be advantageous for the corresponding monoaminacid and corresponding alkenylnitrile to be introduced into the liquid form. This allows for a higher conversion into better spacetime production compared to the processes in which ammonamine is introduced into the gaseous state in the reaction mixture. Therefore, the corresponding alkenylnitrile and the corresponding monoamine are introduced at a suitable temperature and suitable pressure to ensure that these starting materials are present in liquid form for the preparation of the aminoalkylnitrile.

A preferred embodiment of the process of the invention for preparing an aminoalkylnitrile, therefore, preferably involves the introduction of the corresponding alkenylnitrile and the corresponding monoamine in the liquid form.

In addition, it is preferable that, in the addition of the corresponding alkenylnitrile, the reaction stream has a corresponding minimum demoamine excess of 0.1 mol% based on alkenylnitrile. In addition, the molar excess of alkenylnitrile-based monoamine has a value in the range 0.1 to 20%. The value is most preferably in the range of 1 to 10 mol%. In particular, the value is in the range of 2 to 8 mol%.

Excess alkenylnitrile-based monoamine may be obtained by the addition of the two starting materials in the corresponding ratio if the introduction of monoamine is physically effected in the direction of the reaction current prior to the introduction of alkenylnitrile. with alkenylnitrile in the reaction stream occurs in two different dereation regions. This has the advantage that different reaction conditions can be selected for the reaction. In this way the most complete alkenylnitrile reaction can be obtained while simultaneously reducing the proportion of by-products in the reaction stream.

The reaction in step (c) of the process of the invention to prepare an aminoalkylnitrile is preferably carried out so that the alkenylnitrile consumption in the first reaction region is 80 to 98%. This means that the reaction current has a first concentration of alkenylnitrile upon entering the first reaction region, and has a second concentration after leaving the first reaction region, which is such that less than the ratio of the second concentration to the first concentration is 0.8. at 0.98.

Conversion to the first reaction region preferably lies in the range of 90 to 95%.

Preference is also given to the residual content of alkenylnitrile in the reaction stream after the reaction in step (d) of the invention process to prepare an aminoalkylnitrile being less than 1% by weight.

In addition, other reaction regions may be present. In this case, it is sufficient that the last reaction region present in the direction of the reaction current be configured such that the above mentioned residual content of alkenylnitrile in the reaction current is less than 1 % by weight.

When more than two reaction regions are present, the conversion in the first reaction region in the direction of the reaction current may, if appropriate, be less than that indicated above. As set forth above, an advantage in the process of the invention for preparing an aminoalkylnitrile is that the reaction to form alkenylnitrile is carried out in two different reaction regions. As a result, it is possible to select different reaction conditions for the reaction. It has been found to be advantageous for the reaction current in the first and second reaction regions to have different temperatures. In particular, preference is given to the reaction current in the first reaction region in the reaction having a higher temperature than at least in the second reaction region.

The temperature of the reaction stream in the first stripping region is preferably in the range of 20 ° C to 110 ° C. The range is more preferably from 60 ° C to 80 ° C.

The temperature of the reaction stream at least in the second reaction region is preferably in the range of 0 to 100 ° C, in particular in the range of 30 to 60 ° C.

If at least one other reaction region is present, the different, preferably lower, temperature compared to the first reaction region may also be present only in at least one other reaction region.

In addition, pressures in the first and second stripping regions may differ. However, the pressure may likewise be the same, which is preferable. A gauge pressure in the range of 1 bar to 20 bar preferably prevails in the first and second reaction regions. Preferably, therefore, is given the gauge pressure in the first and second reaction regions of the process of the invention for preparing an aminoalkylnitrile, being identical or different, and situating. range from 1bar to 20 bar. The gauge pressure is preferably from 2 to 5 bar. Preference is also given to the corresponding monoamine and corresponding alkenylnitrile feed streams as much as a manometric pressure which is almost as high.

It is known that water added in addition to a C-C double bond monoamine of an alkenylnitrile catalyzes the reaction. Preference is therefore also given to water that is introduced into the reaction chain before the reaction in the first reaction region before the reaction current reaches the first reaction region.

Water may, for example, be introduced into the flow stream in the form of an additional feed stream. In addition, it is possible for at least part of monoamine to be introduced as an aqueous solution into the reaction stream. This may be effected, for example, in the form of an aqueous monoamine solution of 30 to 70 wt%. In addition, the alkenylnitrile used may comprise water.

The process of the invention for preparing an aminoalkylnitrile preferably comprises another step (e) wherein the reaction stream is discharged from the second reaction region after the reaction.

In addition, unreacted monoamine may be separated from the reaction current after the reaction in the second reaction region, or in the second reaction region or outside the second reaction region. This can be done, for example, by distillation. Another vessel, for example a distillation column, may be used for this purpose. Such an unreacted semoamine separation is preferably carried out outside the second deriving region, in particular downstream thereof. Monoamine that has been recovered in this way can be fed back into the reaction current before it reaches the first reaction region. This recirculation may be complete or partial. It is just as conceivable that unreacted monoamine is still processed or disposed of.

The present invention further provides a process for preparing a diamine of a corresponding aminoalkylnitrile comprising steps:

(a) introducing the discharged reaction stream in step (e) of the process of the invention to prepare an aminoalkylnitrile within a reducing region; and

(b) reduction of the aminoalkylnitrile present in the derivative current in the corresponding diamine.

Based on the reaction stream as obtained from the inventive process for preparing an aminoalkylnitrile, after the reaction of at least 2 stages, the present invention further provides the corresponding aminoalkylnitrile reduction in the diamine. Here the nitrile group is thus converted, in a second reaction step, into the oxidizing state of an amine. The product thus obtained comprises not only this amino function, but also another amino function which has been introduced by means of monoamine.

In a preferred embodiment, the reduction is effected by hydrogen. This can be used as such or as part of a gas mixture. The nitrile group of aminoalkylnitrile is thus transformed into a primary amine function.

Ammonia may be introduced into the reaction stream prior to step (b) of the process of the invention to prepare a diamine.

Steps (a) and (b) of the process of the invention for preparing a diamine are preferably performed in a continuous mode of operation.

Particular preference is given to the recirculation of at least part of the crude product formed after reduction in step (b) to form a recycle stream.

When such a recycle stream is present, preference is given to hydrogen and ammonia being used and being introduced into the recycle stream before the discharged reaction stream first step is introduced into the recycle stream.

It is very particularly preferable for the recycle stream to pass through the heat exchanger, which heats the recycle stream after the introduction of ammonia and hydrogen, and prior to the introduction of the discharged stream from the first step.

The molar ratio of ammonia to aminoalkylnitrile is, for example, about 5. When hydrogen is used for hydrogenation, a total pressure in the range of 50 to 300 bar can be established. The total pressure is the sum of the partial pressures of ammonia, aminoalkylnitrile, hydrogen and, if appropriate, unreacted starting materials and formed products, and possibly also water at their temperature, and is advantageously adjusted to the desired value by hydrogen injection. . In a preferred embodiment, steps (a) and (b) of the process of the invention for preparing the diamine are performed in a continuous mode of operation.

A catalyst is advantageously employed, particularly when hydrogen is used. The reduction preferably takes place over a fixed catalyst bed. Operation of the upstream mode or operation of the downstream mode is possible here. Suitable catalysts for the hydrogenation of aminoalkylnitrile in the corresponding diamines are described in EP-B 742 045 or EP-B 892 77. Maximum temperature in the reduction region during reduction is preferably 150 ° C.

As catalysts for the hydrogenation of the nitrile naamine function, it is possible in particular to use catalysts which comprise, as active species, one or more elements of the Periodic Table transition group 8 (Fe, Co, Ni, Ru, Rh, Pd, Os, Ir, Pt), preferably Fe, Co, Ni, Ruou Rh, particularly preferably Co or Ni. These include structural catalysts (also referred to as Raney® type, hereinafter also: Raney catalyst) which are obtained by leaching (activating) a hydrogenating active metal alloy and another component (preferably Al). Catalysts may additionally comprise one or more promoters. Catalysts may be used as allative catalysts or in supported form. The supports used are preferably metal oxides such as Al2 O3, SiO2, ZrO2, T1O2, metal oxide mixtures or carbon (activated carbon, carbon black, graphite).

Prior to use, oxide catalysts are activated outside the reactor or in the reactor by reducing the active metal oxides in a gaseous stream comprising hydrogen at elevated temperature. If catalysts are reduced outside the reactor, passivation by means of a gaseous stream comprising hydrogen or inclusion in an inert material may then be performed in such a way as to avoid uncontrolled oxidation in air and possible safe handling.

Particularly preferred fixed bed catalysts are fully active Mn, P and alkali metal doped cobalt catalysts (Li, Na, K, Rb, Cs) which are set forth in EP-A 1 742 045. Catalytically active catalysts of these catalysts comprise, rather than reducing. with hydrogen, 55 to 98% by weight, in particular 75 to 95% by weight, cobalt, 0.2 to 15% by weight of phosphorus, 0.2 to 15% by weight of manganese, and 0 to 0.05 to 5% by weight of alkali metal, in particular sodium, in each case calculated as oxide.

Other suitable catalysts are catalysts disclosed in EP-A 963 975 which, prior to hydrogen treatment, comprise from 22 to 40 wt% ZrO 2, from 1 to 30 wt% oxygen-containing copper decomposed, calculated as CuO, from 15 to 50% by weight of oxygen-containing nickel compounds, calculated as NiO, with the molar ratio of Ni: Cu being higher than 1, from 15 to 50% by weight of oxygen-containing cobalt compounds, calculated as CoO, from 0 to 10% by weight of oxygen-containing aluminum and / or manganese compounds, calculated as Al2Os or MnO2, and no oxygen-containing molybdenum compounds; for example the catalyst A shown in this document having the composition of 33 wt% Zr calculated as ZrO 2, 28 wt% Ni calculated as NiO, 11 wt% Cu calculated as CuO and 28 wt% of Co, calculated as CoO.

Also suitable are the catalysts disclosed in EP-A696 572, which, prior to hydrogen reduction, comprise from 20 to 85% by weight of ZrC> 2, from 1 to 30% by weight of oxygen-containing copper compounds, calculated as CuO, from 30 to 70% by weight of oxygen-containing nickel compounds, calculated as NiO, from 0.1 to 5% by weight of oxygen-containing molybdenum compounds, calculated as M0O2, and from 0 to 10% by weight of aluminum compounds and / or of magnesium containing oxygen, calculated as Al2O3 or MnO2. Mention may be made by the catalyst example specifically set forth herein which comprises 31.5 wt% ZrO2, 50 wt% NiO, 17 wt% CuO and 1.5 wt% M0O3. Similarly suitable are catalysts described in WO-A 99/44984, which comprises (a) iron or an iron-based compound or mixtures thereof, (b) from 0.001 to 0.3% by weight, based on (a) , of a promoter based on 2, 3, 4 or 5 elementoselected from the group consisting of Al, Si, Zr, Ti, V, (c) from 0 to 0.3% by weight, based on (a), of a alkali metal and / or alkaline earth metal based compound, and (d) from 0.001 to 1% by weight based on (a) demanganese.

Reduction may be performed adiabatically if the manner in which the reaction is performed is appropriate.

The stream obtained from the reduction comprises not only the product but also ammonia and hydrogen, which may, if appropriate, be recirculated after being separated.

The invention further provides an apparatus for preparing an aminoalkylnitrile by reacting a corresponding monoamine with a corresponding alkenylnitrile in a continuous mode of operation comprising

- a first reaction region comprising

- an input provided with a power line, with the power line having a

- a first inlet that is suitable for introducing amonoamine into the feed line;

a second inlet that is suitable for introducing alkenylnitrile into the feed line and is located between the first inlet and the inlet of the first reaction region;

- an output that is connected to the power line; and

- a transfer facility to a second offshore region, and

- a second reaction region, with the feed line comprising aminoalkylnitrile.

The above described apparatus for preparing an aminoalkylnitrile is a preferred apparatus for carrying out the invention process for preparing an aminoalkylnitrile.

The apparatus comprises a first reaction region comprising an inlet provided with a feed line, with the feed line having a first inlet which is suitable for introducing ammonamine into the feedline, and a second inlet which is suitable for introducing alkenylnitrile into the supply line. food. The second input is located between the first input and the first reaction region input. In addition, the first reaction region has an output that is connected to the power line. This enables the process of the invention to prepare an aminoalkylnitrile to be carried out in a continuous recycling mode or the apparatus of the invention for preparing an aminoalkylnitrile to be operated. Finally, the first reaction region has a transfer facility that leads to a second reaction region. Accordingly, the apparatus of the invention for preparing an aminoalkylnitrile thereof forms a second reaction region. The apparatus of the invention for preparing an aminoalkylnitrile comprises aminoalkylnitrile in the feed line. The latter ensures that when alkenylnitrile is introduced through the second inlet, it is diluted by aminoalkylnitrile and no introduction of alkenylnitrile into pure monoamine therefore occurs.

The first and second reaction regions of the inventive apparatus for preparing an aminoalkylnitrile may be present as different zones in a reactor vessel. However, preference is given to the first and second reaction regions being different dereation vessels or a cascade of vessels.

These two reactor vessels may be connected to one another by means of a tube.

Furthermore, the present invention further provides an apparatus for preparing a diamine from a corresponding aminoalkylnitrile comprising

an apparatus for preparing an aminoalkylnitrile as described above; and

- a reduction region.

The reducing region is preferably a fixed bed reactor.

As set forth above, the apparatus of the invention for preparing an aminoalkylnitrile is a preferred apparatus for performing a process according to the invention for preparing an aminoalkylnitrile.

The present invention therefore further contemplates the use of an apparatus according to the invention for preparing an aminoalkylnitrile by matching a corresponding monoamine with a corresponding alkenylnitrile in a continuous mode of operation.

Furthermore, the apparatus of the invention for preparing a diamine is suitable for carrying out the process of the invention for preparing a diamine.

Accordingly, the invention further contemplates the use of an apparatus according to the invention to prepare a corresponding aminoalkylnitrile diamine. The invention is illustrated by the following figures and examples.

In the figures,

Figure 1 shows a schematic flowchart for an illustrative process for preparing an aminoalkylnitrile according to the present invention, and

Figure 2 shows a schematic flowchart for preparing a diamine of a corresponding aminoalkylnitrile according to the present invention.

Figure 1 shows the reaction step of monoamine with alkenylnitrile to form the corresponding aminoalkylnitrile. Here, in a recycle mode of the operation, monoamine is introduced through inlet 1 and alkenylnitrile is introduced through inlet 2 into the recycle stream. Actual monamine amination with alkenylnitrile occurs in reactor 5 through a tube that provides a heat exchanger 3 between input 2 and reactor 5. Reaction chain present in reactor 5 is partially recirculated by means of a pump 4 in the recycle stream, and the uncirculated portion of the flow current is transferred through heat exchanger 6 to a second reactor 7. This enables the reaction current in reactors 5 and 7 to have different temperatures. The reaction stream comprising aminoalkylnitrile leaves reactor 7 through outlet 8.

Figure 2 presents the reduction step with the aid of hydrogen. Aminoalkylnitrile from outlet 8 is transferred through inlet 14 to a fixed bed reactor 15 via a tube. Here, the catalyst leitofix causes the nitrile group to be reduced by hydrogen. This is introduced through inlet 12. Ammonia is introduced through inlet 11, and the reaction current is conducted in such a way that it flows through a exchanger. after the addition of hydrogen and daamonia to heat it before aminoalkylnitrile enters reactor 15 via inlet 14. This has in particular the advantage that aminoalkylnitrile is reacted very rapidly in reactor 15 and therefore fear only a very short residence time before it contacts the hydrogenation catalyst. This results in less byproduct (bisdiamine) being formed. The reaction current flows through the fixed delight reactor 15 from top to bottom (downflow mode) and through heat exchanger 17 to separator 18, in which the crude product is separated from hydrogen, monoamine and ammonia, and can be discharged through outlet 20. In addition, at least part of the crude product can be recirculated to the reaction stream via pump 16. At least partial recirculation results in a hydrogenation recycling process, too, which is preferred. The obtained mixture of hydrogen, monoamine and ammonia can be discharged through outlet 19.

EXAMPLES

EXAMPLE 1

DMA addition to ACN is performed in a continuously operated cascade of agitated vessels comprising three agitated vessels. The volume ratio of the three shaken vessels is 1: 1.5: 2.5. Sandblasting is performed at a pressure of 5 bar.

The temperature in the first two shaken vessels is 60 ° C, and that in the third vessel is 30 ° C. The addition reaction is performed in one production, calculated as acrylonitrile feed per unit time, based on the volume of the first agitated vessel, 0.54 kg / liter / hour. Molar ratio of DMA starting material to ACN is 0.98. The residual content of acrylonitrile is 3% by weight (based on the total reaction product mixture). The average residence time of the reaction mixture in the vessels of the addition reaction stage is about 4 hours.

The reaction product mixture of the addition reaction stage is continuously hydrogenated through a fixed bed catalyst containing cobalt in a continuously operated reaction at a second stage of reaction. The spatial velocity through the catalyst is 1.0 kg (DMAPN gross output) / kg (catalyst) / hour. Hydrogenation is performed at an absolute pressure of 180 bar. The reactor outlet temperature is 120 ° C. Massing of the circulation current for the supply of DMAPN is 2,5 kg / kg. The ratio of ammonia in the feed to the reaction is 0.8 kg (ammonia) / kg (DMAPN), and the molar ratio of ammonia to nitrile is 5.

After a total operating period of 1300 hours, a considerable advance of nitrile is observed on hydrogenation (> 0.1% nasaphosphate DMAPN).

EXAMPLE 2

The addition of the DMA over the ACN is performed in a continuously operated agitated devas cascade comprising seven agitated vessels. The volume ratio of the seven agitated vessels is 1: 1.5: 2.5: 3.4: 3.4: 3.4: 3.4. Sandblasting is performed at a pressure of 5 bar.

The temperature in the first two agitated vessels is 60 ° C, and that in the third to seventh vessels is 40 ° C. The addition reaction is performed in one production, calculated as unitary acrylonitrile feed, based on the volume of the first agitated vessel, 0.54kg / liter / hour. The molar ratio of DMA starting material to ACN is 0.98. The residual acrylonitrile content is about 2% by weight (based on total reaction product mixture). The average residence time of the reaction mixture in the vessels of the addition reaction stage is about 16 hours.

After a 500 hour operating period, a reduced amount of DMA is added to the addition reactor for about 24 hours, which leads to the residual acrylonitrile content in the product mixture rising from 5 to 30% by weight.

The reaction product mixture of the addition reaction stage is continuously hydrogenated through a fixed bed catalyst containing copper in a continuously operated reactor in a second stripping stage. The spatial velocity through the catalyst is 1.0 kg (DMAPN gross output) / kg (catalyst) / hour. Hydrogenation is performed at an absolute pressure of 180 bar. The reactor outlet temperature is 120 ° C. Massing of the circulation current for the supply of DMAPN is 2,5 kg / kg. The ratio of ammonia in the feed to the reaction is 0.8 kg (ammonia) / kg (DMAPN), and the molar ratio of ammonia to nitrile is 5.

No advance of nitrile is detected at the exit of the hydrogenation stage within the first 500 hours of operation.

After a total operating period of 530 hours, a noticeable advance of nitrile is observed in hydrogenation (> 0.2% nasaphosphate DMAPN).

EXAMPLE 3

DMA addition over ACN is performed in a continuously operated cascade of agitated vessels comprising three agitated vessels. The volume ratio of the three shaken vessels is 1: 1.5: 2.5.

The reaction is performed at a pressure of 5 bar. The temperature in the first two stirred vessels is 60 to 80 ° C, and that in the third vessel is 30 to 45 ° C. The addition reaction is performed in a production, calculated as acrylonitrile feed per unit time, based on the volume of the first stirred vessel, from 0.44 to 0.54 kg / liter / hour. The starting molar ratio of DMA to ACN is 1.08 to 1.18. Residual deacrylonitrile content is less than 0.2% by weight (based on the total mixture of the reaction product). The average residence time of the stirring mixture in the vessels of the addition reaction stage is about 4 hours. The reaction product mixture of the addition reaction stage is continuously hydrogenated through a fixed bed catalyst containing a high reactor in a continuously reactor. operated on a second stage dereation. The spatial velocity through the catalyst is 1.0 kg (DMAPN gross output) / kg (catalyst) / hour. Hydrogenation is performed at an absolute pressure of 180 bar. The reactor outlet temperature is 120 ° C. Massing of the circulation current for the supply of DMAPN is 2,5 kg / kg. The ratio of ammonia in the feed to the reaction is 0.8 kg (ammonia) / kg (DMAPN), and the molar ratio of ammonia to nitrile is 5.

No advance of nitrile in hydrogenation is observed within a 600 hour operating period.

EXAMPLE 4

The DMA addition reaction over ACN is performed in a continuously operated urine containing a pumped circuit having two vessels, and one vessel through which laminar flow occurs, and two other vessels. The volume ratio of vessels in the pumped circuit to the vessel through which the laminar flow occurs and the two other vessels is 1: 0.2: 2: 3.

The temperature in the pumped circuit is 60 ° C, and that in other vessels is 30 to 45 ° C. The addition reaction is performed in a production, calculated as acrylonitrile feed per unit time, based on the volume of the pumped circuit, 0.75 kg / liter / hour. The ratio of the amount of crude DMAPN pumped through the first two vessels to the reaction product mixture is 30 kg / kg.

The molar ratio of DMA to ACN starting material is 1.08. The residual content of acrylonitrile is less than 0.1% by weight (based on the total reaction product mixture) in the reaction stream after the 5th vessel. The average residence time of the nasous reaction mixture from the addition reaction stage is about 4 hours. The reaction is carried out at a pressure of 4 bar. The acrylonitrile used has a water content of about 0.4%.

The reaction product mixtures of the death reaction stage are continuously hydrogenated through a fixed bed catalyst containing cobalt in a reactor continuously operated at a second reaction stage. The average spatial velocity is 1.0 kg (DMAPN gross output) / kg (catalyst) / hour. Hydrogenation is carried out at 180 bar absorbent pressure. The reactor outlet temperature is about 144 ° C. Massing of the circulation current for the supply of DMAPN is 2,5 kg / kg. The ratio of ammonia in the feed to the reaction is 0.8 kg (ammonia) / kg (DMAPN), and the molar ratio of ammonia to nitrile is 5.

No advance of nitrile in hydrogenation is observed within an operating period of 6 months; during this time a total amount of about 4500 kg (DMAPN) / kg (catalyst) is hydrogenated.

Claims (33)

1. A process for preparing an aminoalkyl nitrile by reacting a corresponding monoamine with a corresponding alkenyl nitrile in a continuous mode of operation, the process comprising the steps of: (a) feeding the corresponding monoamine into a continuously conducted reaction current; of the corresponding alkenylnitrile in a reaction chain, with it already comprising the aminoalkylnitrile and addition, (c) reacting the reaction current in a first reaction region, and (d) at least partially transferring the reaction current to at least a second reaction region for another reaction. Process according to Claim 1, characterized in that the aminoalkylnitrile is 3-dimethylaminopropionitrile. Process according to claim 1 or 2, characterized in that at least steps (a) to (c) are carried out in the recycling mode. Process according to any one of claims 1 to 3, characterized in that the alkenylnitrile and monoamine are introduced in liquid form. A process according to any one of claims 1 to 4, characterized in that, in addition to the corresponding alkenylnitrile, the reaction chain has a corresponding minimum monoamine excess of -0.1 mol%, based on alkenylnitrile. Process according to any one of claims 1 to 5, characterized in that the reaction in step (c) is carried out such that the consumption of alkenylnitrile is in the range of 80 to 98%. Process according to any one of claims 1 to 6, characterized in that the residual content of the reaction current alkenylnitrile after the reaction in step (d) is less than 1% by weight. Process according to any one of claims 1 to 7, characterized in that the reaction current in the first and second reaction regions in the reaction has different temperatures. Process according to any one of claims 1 to 8, characterized in that the reaction current in the first reaction region in the reaction has a higher temperature than in the small reaction region. Process according to any one of claims 1 to 9, characterized in that the temperature of the reaction stream in the first reaction region is in the range of 20 ° C to 110 ° C. Process according to any one of claims 1 to 10, characterized in that the temperature of the reaction stream in the least second reaction region is in the range 0 to 100 ° C. Process according to any one of claims 1ali, characterized in that the gauge pressures in the first and second reaction regions are identical or different and are in the range from -1 bar to 20 bar. Process according to any one of claims 1 to 12, characterized in that water is introduced into the reaction stream prior to the reaction in the first reaction region. Process according to any one of claims 1 to 13, characterized in that the monoamine is introduced as an aqueous solution into the reaction stream. Process according to any one of claims 1 to 14, characterized in that the unreacted monoamine is separated from the reaction current after the reaction in the second reaction region or outside the second reaction region. Process according to any one of claims 1 to 15, characterized in that it comprises the additional step: (e) discharging the reaction current from the second reaction region after the reaction. A process for preparing a corresponding aminoaminoalkylnitrile diamine, characterized in that it comprises steps: (a) introducing the discharged reaction stream in step (e) of claim 16 into a reducing region; and (b) reducing the aminoalkylnitrile present in the derivative current in the corresponding diamine. Process according to Claim 17, characterized in that the reduction is effected by hydrogen. Process according to Claim 17 or 18, characterized in that the ammonia is introduced into the reaction stream before step (b). Process according to any one of claims 17 to 19, characterized in that steps (a) and (b) are performed in a continuous mode of operation. Process according to claim 20, characterized in that the crude product of step (b) according to claim-17 is at least partially recirculated in a recycle stream. Process according to any one of claims 18, 19 and 21, characterized in that hydrogen and ammonia are introduced into the recycle stream in the direction of the recycle stream prior to the introduction of the reaction stream in step (a). ) of claim 17. A process according to claim 22, characterized in that the recycle stream flows through a heat exchanger to heat it after introduction of hydrogen and ammonia, and prior to introduction in step (a) of claim 17. Process according to any one of claims 17 to 23, characterized in that the reduction is carried out by means of a fixed bed catalyst. Process according to any one of Claims 17 to 24, characterized in that the maximum temperature in the reducing region during reduction is 150 ° C. Process according to any one of Claims 17 to 25, characterized in that the reduction is carried out adiabatically. 27. Apparatus for preparing an aminoalkylnitrile by blasting a corresponding monoamine with a corresponding alkenylnitrile in a continuous mode of operation, the apparatus comprising a first reaction region comprising: - an inlet provided with a feed line, with the feedline having: - a first inlet that is suitable for introducing ammonamine into the feedline - a second inlet that is suitable for introducing alkenylnitrile into the feedline, and is located between the first inlet and the first reaction region inlet; - an output that is connected to the power line; a transfer facility for a second reaction region, and a second reaction region, with the feed line comprising aminoalkylnitrile. Apparatus according to claim 28, characterized in that the first and second reaction regions are reactorifferent vessels. Apparatus according to claim 28, characterized in that the transfer installation between the various reactor vessels is a tube. Apparatus for preparing a corresponding aminoalkylnitrile diamine, characterized in that it comprises an apparatus as defined in any one of claims 27 to 29; e- a region of reduction. Apparatus according to claim 30, characterized in that the reduction region is a fluid bed reactor. Use of an apparatus as defined in any one of claims 27 to 29, the use of which is for preparing an aminoalkylnitrile by reacting a corresponding monoamine with a corresponding alkenylnitrile in a continuous mode of operation. Use of an apparatus as defined in claims 30 or 31, the use characterized in that it is for preparing a corresponding aminoaminoalkyl nitrile diamine.